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• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
  • C07C4/08—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule
  • C07C4/12—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule from hydrocarbons containing a six-membered aromatic ring, e.g. propyltoluene to vinyltoluene
  • C07C4/14—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule from hydrocarbons containing a six-membered aromatic ring, e.g. propyltoluene to vinyltoluene splitting taking place at an aromatic-aliphatic bond
  • C07C4/18—Catalytic processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
  • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
  • B01J21/04—Alumina
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
  • B01J23/8926—Copper and noble metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
  • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/8946—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali or alkaline earth metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/90—Regeneration or reactivation
  • B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the noble metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/12—Oxidising
  • B01J37/14—Oxidising with gases containing free oxygen
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/22—Halogenating
  • B01J37/24—Chlorinating
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J38/00—Regeneration or reactivation of catalysts, in general
  • B01J38/02—Heat treatment
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J38/00—Regeneration or reactivation of catalysts, in general
  • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
  • B01J38/08—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using ammonia or derivatives thereof
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J38/00—Regeneration or reactivation of catalysts, in general
  • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
  • B01J38/10—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using elemental hydrogen
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J38/00—Regeneration or reactivation of catalysts, in general
  • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
  • B01J38/12—Treating with free oxygen-containing gas
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J38/00—Regeneration or reactivation of catalysts, in general
  • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
  • B01J38/42—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using halogen-containing material
  • B01J38/44—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using halogen-containing material and adding simultaneously or subsequently free oxygen; using oxyhalogen compound
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
  • C07C4/08—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule
  • C07C4/12—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule from hydrocarbons containing a six-membered aromatic ring, e.g. propyltoluene to vinyltoluene
  • C07C4/14—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule from hydrocarbons containing a six-membered aromatic ring, e.g. propyltoluene to vinyltoluene splitting taking place at an aromatic-aliphatic bond
  • C07C4/20—Hydrogen being formed in situ, e.g. from steam
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
  • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
  • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
  • C07C2523/46—Ruthenium, rhodium, osmium or iridium
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/584—Recycling of catalysts
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
  • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y10S502/00—Catalyst, solid sorbent, or support therefor: product or process of making
  • Y10S502/515—Specific contaminant removal
  • Y10S502/517—Sulfur or sulfur compound removal

Definitions

• the present invention relates to petrochemical processing, and more particularly, to methods for regeneration of rhodium-containing catalysts.
• the invention is particularly concerned with methods for regeneration of rhodium-containing catalysts for dealkylating alkyl benzenes.
• the process is carried out at a temperature of from 400° to 500° C. and at a pressure up to 30 atm using individual alkyl aromatic hydrocarbons or their mixtures with hydrocarbons of other classes as a raw material.
• Dealkylation of aromatic hydrocarbons with steam is carried out using catalysts containing noble metals of Group VIII of the Periodic System, preferably rhodium, applied to alumina (Cf. USSR Inventor's Certificate No. 229,477, Int. Cl. CO7c 15/04, published Mar. 22, 1972).
• alkali metals, alkaline-earth metals as well as metals belonging to the group of copper, ferrum, chrome and lanthanum are introduced into the catalyst composition (Cf. British Pat. No. 1,313,941, Int. Cl. CO7c 3/58, patented Apr. 18, 1973; U.S. Pat. Nos. 3,436,433 and 3,436,434, Int. Cl. CO7c 3/58, BO1j 21/04, patented Apr. 1, 1969; U.S. Pat. Nos. 3,649,706 and 3,649,707, Int. Cl. CO7c 3/58, BO1j 21/04, patented Mar. 14, 1972; U.S. Pat. No. 3,848,014, Int. Cl. CO7c 3/58 patented Nov. 12, 1974).
• Rhodium-containing catalysts are also used to conduct the reaction of dealkylation with hydrogen (hydrodealkylation).
• Also known in the art is a method for regenerating a rhodium-containing catalyst, residing in treating it with either a nitrogen-oxygen mixture or air-steam mixture in order to burn out coke, followed by chlorination at a temperature between 400° and 600° C. with a nitrogen-oxygen mixture containing 0.1 to 0.2 g/l of chlorine or a chlororganic compound.
• the catalyst is then reclaimed in a flow of hydrogen at a temperature of from 450° to 550° C. followed by treatment of the catalyst with steam at a temperature of from 400° to 500° C. and further using it in the process of dealkylation (Cf. USSR Inventor's Certificate No. 448,671, Int. Cl. BO1j 11/58, published Mar. 15, 1978).
• Activity of the regenerated catalyst increases in case a chlorine-containing gaseous mixture used in the chlorination stage contains, in addition, water vapour in an amount of 0.002 to 0.1 g/l (Cf. USSR Inventor's Certificate No. 627,849, Int. Cl. BO1j 11/68, published Oct. 15, 1978).
• the principal object of the present invention is to increase the life of rhodium-containing catalysts by treating sulphur-poisoned catalysts with reagents allowing for the removal of sulphur from the catalyst surface.
• a method for regenerating rhodium-containing catalyst used for dealkylating alkyl benzenes by conversion with steam or hydrogen comprising the steps of burning out carbon deposits by an oxygen-containing gas, chlorinating the catalyst with chlorine or with a chlororganic compound in a flow of hydrogen, an inert gas, or a mixture of an inert gas with oxygen and moisture, wherein, according to the invention, the catalyst is additionally treated at a temperature of from 20° to 650° C., at a pressure of 1 to 50 atm, during 0.5 to 48 hours with liquid ammonia in the form of an aqueous solution, or in the gaseous ammonia per se, or in the form of a nitrogen-containing compound capable of decomposing under said treatment to yield ammonia.
• the treatment with ammonia in the gaseous phase is conducted in the presence of at least one component selected from the group consisting of: water, hydrogen, or a nitrogen-oxygen mixture.
• gaseous mixture components in addition to ammonia, water or steam, hydrogen, and nitrogen-oxygen mixtures are used.
• Such compounds as ethanol form water and hydrogen on a catalyst in a process of dehydration and dehydrogenation can also be used.
• Nitrogen-oxygen mixtures as noted herein can contain a different quantity of oxygen varying from technical nitrogen comprising usually 1% vol. of O 2 to air. Mixtures of oxygen with inert gases as well as with CO 2 can also be used. Instead of ammonia, some of compounds such as ammonium chloride, an alkylammonium compound, ethanolamine, hydroxylamine or a salt of hydroxylamine chlorhydrate, which form ammonia while decomposing can be used. The use of chlorine-containing compounds of ammonia makes it possible to combine the process of desulphuration of a catalyst with its chlorination.
• the catalyst is treated with ammonia either in a gaseous or liquid state.
• the catalyst treatment with ammonia is an essential stage in the regeneration process of the rhodium-containing dealkylation catalysts reducing their activity in a reaction cycle.
• the regeneration process should include an ammonia treatment stage, carbon burning-out and chlorination.
• Such intermediate operations as catalyst reduction and calcination can be carried out between the operative steps.
• the catalyst treatment with ammonia in the gaseous phase is carried out by passing ammonia together with steam, hydrogen, and a nitrogen-oxygen mixture through a catalyst.
• ammonia treatment can be carried out in sequence varying with reference to other regeneration on stages.
• a gaseous phase treatment is carried out preferably at a temperature from 150° to 650° C. and pressure of between 5 and 15 atm.
• ammonia treatment in combination with the above mentioned components is more effective than with ammonia alone.
• the ammonia concentration should be sufficiently high. It is preferable to use mixtures with an ammonia concentration of 20-95% vol.
• Aqueous ammonia is used for treatment in a liquid phase.
• a rise in temperature favors more complete sulphur removal, but for liquid phase treatment at a temperature above 200° C., pressure above 15 atm is needed to the detriment of catalytic properties of a catalyst. Therefore, the preferable temperature interval for treatment ranges from room temperature to 200° C. It is possible to carry out ammonia treatment at a temperature lower than room temperature but it is inconvenient due to the necessity to cool the catalyst and solution used for treatment.
• the pressure should vary from 1-15 atm, to ensure carrying out the treatment in a liquid phase.
• the duration of ammonia treatment is governed by ammonia content.
• the treatment duration ranges from 0.5 to 5 hours.
• the complete removal of sulphur can be achieved in a time of less than 0.5 hour, but this is technologically unwarranted.
• a decrease in ammonia content results in an increase of time necessary to remove sulphur from a catalyst up to 24-48 hours.
• Ammonia concentration in aqueous solutions can vary in a wide range, from 0.01 mass % up to a saturated ammonia solution but it is preferable to use solutions having concentrations of 0.5-5 weight %.
• Ammonia treatment can be carried out at any stage of regeneration, but it is advisable to treat catalysts wherein metallic components are in oxidized form, i.e. after the carbon burning-out stage or chlorination stage.
• the process of dealkylation is carried out by passing alkyl benzenes or their mixtures with hydrocarbons of other classes and steam or hydrogen at a temperature of from 450° to 650° C. and at a pressure of 5-10 atm through a catalyst situated in a flow reactor.
• the regeneration cycle is carried out either directly in the reaction vessel for dealkylation or in a separate apparatus.
• the regeneration cycle involves burning-out coke deposits by an oxygen-containing inert gas, chlorinating step with chlorine or chlororganic compound in a flow of hydrogen, an inert gas or a mixture of an inert gas with oxygen and moisture, and an ammonia treatment stage.
• the sequence of the above mentioned stages can be varied and it is possible to carry out intermediate reduction or calcination of the catalyst after any of the operative steps.
• the catalyst is reduced by hydrogen and reused in a process of dealkylation.
• the toluene that was used contained 4 ⁇ 10 -5 weight % of sulphur-containing compounds based on sulphur.
• the catalyst composition in % by weight is as follows: rhodium, 0.6; copper, 0.3; potassium, 2.5; the balance being alumina.
• the catalyst testing procedure was carried out in a steel flow reactor 36 mm in diameter provided with a pocket for thermocouples 8 mm in diameter. 60 cm 3 of the catalyst were charged into the reactor and reduced with hydrogen fed at a rate of 100 l/h with a gradual increase (during 8 hours) in temperature up to 500° C., and held at this temperature for 2 hours. Upon termination of the reduction, a required testing temperature was set, whereupon toluene and water or toluene and hydrogen (in hydrodealkylation experiments) were fed into the reactor.
• Liquid products were condensed in a cooler, whereupon gaseous products were separated in a gas separator.
• Product analysis was carried out by the gas chromatography method.
• the catalyst was found to include 5.2 mass % of carbon deposits (coke) and 0.08 mass % of sulphur.
• the regeneration process was carried out as follows. 60 cm 3 of the catalyst was treated directly in the reactor at 550° C. and a pressure of 30 atm with a mixture of ammonia, steam and hydrogen in the ratio of 1:2.5:6.5. To attain the objectives mentioned above an aqueous ammonia containing 28% ammonia, and hydrogen are passed through 60 cm 3 of the catalyst at a rate of 20 ml/h and 50 l/h, respectively. The duration of the treatment is 24 hours. Then the catalyst undergoes oxidative regeneration in order to burn-out coke. Coke burning-out was carried out at elevated temperatures ranging from 300° to 500° C. in a flow of nitrogen-oxygen mixture (technical nitrogen) containing 1% vol. of oxygen, space velocity of the feed mixture being 1,000 h -1 .
• nitrogen-oxygen mixture technical nitrogen
• Chlorination of the catalyst was carried out in a quartz reactor 32 mm in diameter provided with a pocket for thermocouples 8 mm in diameter.
• the catalyst was heated to 550° C. in a flow of technical nitrogen.
• nitrogen was passed through a vessel with water up to moisture saturation, while chlorine obtained by electrolysis of an aqueous solution of sodium chlorite on platinum electrodes was supplied through a separate line.
• Steam-gas mixture containing 1% vol. of chlorine, 2% vol. of steam, 1% vol. of oxygen and the balance being nitrogen, was formed in the reactor. Space velocity of gas feed is 200 h -1 , and time of chlorination is 6 hours.
• the catalyst Upon termination of the chlorination, the catalyst was cooled in a flow of nitrogen to room temperature, whereupon the catalyst was reloaded into a test unit for testing in the process of dealkylation. Before being tested the catalyst was reduced at 500° C. in a flow of hydrogen supplied at space velocity of 500 h -1 .
• the catalyst comprised 0.015 mass % of sulphur (sulphur content prior to regeneration cycle was 0.08 mass %).
• Example 1 60 cm 3 of the spent catalyst similar to that of Example 1 underwent a regeneration cycle similar to that of Example 1 exluding desulphuration of the catalyst.
• a catalyst was composed of the following components in mass %: rhodium, 0.6; ferrum, 2.0; potassium, 1.5; the balance being alumina.
• the catalyst was spent in the process of toluene demethylation with steam.
• Water used for dealkylation contained 7.5 ⁇ 10 -3 mass % of sulphuric acid.
• Dealkylation conditions were the following: temperature, 520° C.; space velocity of toluene feed, 2.7 h -1 ; water-toluene molar ratio 3, duration of the process with sulphur containing raw material, 24 hours. Yield in mass % of benzene toluene converted before sulphur poisoning was 61.2 and that of a liquid product, 84.0. Yield in mass % of benzene after sulphur poisoning of the catalyst was 17.3 and that of a liquid product was 95.0. Sulphur content in the catalyst was 0.1 mass %. 60 cm 3 of the catalyst underwent oxidative regeneration cycle in a flow of technical nitrogen (1% vol of O 2 ) at 500° C.
• the catalyst (30 cm 3 ) comprising 0.3 mass % of rhodium and 0.3 mass % of platinum on an active aluminum oxide was tested in the reaction of toluene hydrodementhylation at atmospheric pressure, temperature of 510° C., space velocity of toluene feed 2.5 h -1 and hydrogen-toluene molar ratio of 4. Under testing conditions the catalyst was poisoned by toluene contaminated by sulphur and containing 2 ⁇ 10 -2 mass. % of sulphur in the form of thiophene. The duration of the experiment was 8 hours. Yield in mass % of benzene on toluene converted before poisoning was 67, after poisoning, 21.
• Example 5 A sample of the catalyst which was poisoned by sulphur as described in Example 5 underwent the regeneration cycle under conditions of Example 5 except for a desulphuration stage which was performed by passing dry ammonia alone at 150° C., a pressure of 7 atm and space velocity of ammonia feed of 900 h -1 for 10 hours. Testing the catalyst in the hydrodemethylation process of toluene under conditions of Example 5 led to a benzene yield of 30 mass % and a liquid product yield of 94.0 mass %. The catalyst treatment by ammonia alone revealed a relatively poor effect of regeneration.
• Example 1 The catalyst of Example 1 was regenerated. All procedures were the same as those of Example 1 except for the ammonia treatment stage. The above mentioned treatment was carried out at 650° C., a pressure of 50 atm for 48 hours under ammonia, steam and hydrogen in a ratio of 1:2.5:6.5. In testing under conditions of Example 1 the yield in mass % of benzene on treated toluene was 40.1 and that of a liquid product, 92.0. The regeneration cycle resulted only in a partial reduction of catalyst activity. The reason for an incomplete activity reduction of the catalyst was likely to relate to excessively severe conditions of the treatment.
• Used as a raw material for dealkylation was a mixture of pyrolysis petroleum fractions, comprising in mass %: non-aromatic hydrocarbons, 4.6; benzene, 15.6; toluene, 65.2; aromatic hydrocarbons C 8 , 6.6; aromatic hydrocarbons C 9 , 8.0.
• the process of dealkylation of the above mentioned raw material was carried out on a fresh catalyst of Example 3 at 490° C., pressure of 7 atm, space velocity of the raw material feed of 1.3 h -1 , water-raw material mass ratio being 1.18.
• the experiments after sulphur poisoning of the catalyst as well as its regeneration were carried out under the conditions of Example 3.
• the herein-proposed method for regeneration can be employed on a commercial scale to reduce activity of rhodium-containing catalysts of alkyl benzene dealkylation process with steam and hydrogen.
• the present invention makes it possible to provide reduction of a rhodium-containing catalyst with any promoter additions regardless the full composition of said catalyst. It is due to the fact that the present invention makes it possible to reduce the properties of rhodium which is an active component of the catalyst.
• the kind of sulphur-containing compounds in a raw material that caused catalyst poisoning is of no importance for the present invention.

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• 1979
  • 1979-06-15 SU SU792770904A patent/SU910184A1/ru active
• 1980
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